US5611682A - Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces - Google Patents

Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces Download PDF

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Publication number
US5611682A
US5611682A US08/523,988 US52398895A US5611682A US 5611682 A US5611682 A US 5611682A US 52398895 A US52398895 A US 52398895A US 5611682 A US5611682 A US 5611682A
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United States
Prior art keywords
fuel
flame
burner
precombustor
passage
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Expired - Lifetime
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US08/523,988
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English (en)
Inventor
Aleksandar G. Slavejkov
Thomas M. Gosling
Robert E. Knorr, Jr.
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Air Products and Chemicals Inc
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Air Products and Chemicals Inc
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Assigned to AIR PRODUCTS AND CHEMICALS, INC. reassignment AIR PRODUCTS AND CHEMICALS, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GOSLING, THOMAS MICHAEL, KNORR, ROBERT ELLSLWORTH, JR., SLAVEJKOV, ALEKSANDAR GEORGI
Priority to US08/523,988 priority Critical patent/US5611682A/en
Priority to TW085107157A priority patent/TW316286B/zh
Priority to KR1019960026682A priority patent/KR100249051B1/ko
Priority to CA002184459A priority patent/CA2184459C/en
Priority to BR9603633A priority patent/BR9603633A/pt
Priority to EP96114157A priority patent/EP0762050B1/en
Priority to ES96114157T priority patent/ES2186751T3/es
Priority to DE69624762T priority patent/DE69624762T2/de
Priority to ZA9607469A priority patent/ZA967469B/xx
Priority to CNB961128143A priority patent/CN1134610C/zh
Publication of US5611682A publication Critical patent/US5611682A/en
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    • C—CHEMISTRY; METALLURGY
    • C03—GLASS; MINERAL OR SLAG WOOL
    • C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
    • C03B5/00—Melting in furnaces; Furnaces so far as specially adapted for glass manufacture
    • C03B5/16—Special features of the melting process; Auxiliary means specially adapted for glass-melting furnaces
    • C03B5/235—Heating the glass
    • C03B5/2353—Heating the glass by combustion with pure oxygen or oxygen-enriched air, e.g. using oxy-fuel burners or oxygen lances
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
    • F23C6/045—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection with staged combustion in a single enclosure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
    • F23D14/22—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/32—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid using a mixture of gaseous fuel and pure oxygen or oxygen-enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2201/00—Staged combustion
    • F23C2201/10—Furnace staging
    • F23C2201/101—Furnace staging in vertical direction, e.g. alternating lean and rich zones
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D2900/00—Special features of, or arrangements for burners using fluid fuels or solid fuels suspended in a carrier gas
    • F23D2900/00012—Liquid or gas fuel burners with flames spread over a flat surface, either premix or non-premix type, e.g. "Flächenbrenner"
    • F23D2900/00013—Liquid or gas fuel burners with flames spread over a flat surface, either premix or non-premix type, e.g. "Flächenbrenner" with means for spreading the flame in a fan or fishtail shape over a melting bath
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/50—Glass production, e.g. reusing waste heat during processing or shaping
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/50—Glass production, e.g. reusing waste heat during processing or shaping
    • Y02P40/57—Improving the yield, e-g- reduction of reject rates

Definitions

  • the present invention pertains to oxy-fuel methods and devices for producing elevated temperatures in industrial melting furnaces for such diverse products as metals, glass, ceramic materials and the like.
  • oxy-fuel glass melting technology One cost effective method for controlling emissions as well as reducing capital requirements is the implementation of oxy-fuel glass melting technology.
  • Use of oxy-fuel in glass melting eliminates nitrogen in the melting process and reduces NO X and particulate emissions to below the levels set by the Environmental Protection Agency (EPA).
  • EPA Environmental Protection Agency
  • oxy-fuel combustion reduces carbon dioxide emissions and brings numerous other benefits ranging from increased production capacity to savings in the amount of batch chemicals required.
  • oxy-fuel burners in glass melting permits the burner designer to achieve varying flame momentum, glass melt coverage and flame radiation characteristics.
  • Different burners produce different levels of NO X in furnaces where nitrogen is present from air leakage, low-purity oxygen supplied from a vacuum swing or pressure swing adsorption unit, nitrogen in the fuel, or nitrogen contained in the batch chemicals.
  • Non-compliance with NO X emission standards, rules and regulations can lead to very large penalties and fines, substantial capital expenditure for clean-up technology, or require the purchase of NO X credits.
  • Another problem with conventional oxy fuel burners is related to the relatively low luminosity of an oxygen-natural gas flame. Radiation from such flames comes from the combustion products, water vapor and carbon dioxide, radiating predominantly wavelengths which are absorbed by the surface of the glass melt. This adversely affects the overall heat transfer as this surface absorbed heat is re-radiated not only where it needs to go, i.e. down into the lower layers of the glass melt, but also back up towards the furnace crown. In contrast, luminous flames radiate a significant portion of radiation in the wavelengths that penetrate glass, thus making it easier to deliver heat to the lower layers of the melt.
  • U.S. Pat. No. 4,927,357 discloses a gas-injection lance, burner which produces a flame by having an elongated fuel jet which entrains air from a port above the fuel jet intersecting an elongated gas (oxygen) jet inside a furnace to produce a flame flattening effect.
  • the burner contains a fuel passage having a generally elongated cross-section which is surrounded by a housing having a complementary cross-section, the housing being larger than the fuel passage to create a passage between the housing and the fuel passage.
  • the housing and the fuel passage have a common end which lies in a plane generally perpendicular to the axis of the burner, to thus produce the flat flame which can be made fuel-rich by controlling the amount of oxidizer (oxygen) introduced into the oxygen passage.
  • an elongated oxidizer passage Disposed beneath the common end of the fuel and the oxidizer passages is an elongated oxidizer passage which is adapted to introduce oxygen underneath the fuel-rich flame produced by the upper portion of the burner to thus achieve the fuel-rich flame overlying the fuel-lean flame.
  • a precombustor or burner block can be disposed on the flame end of the burner to further enhance operating characteristics of the burner.
  • the precombustor or burner block contains an oxidizer passage which is of a complementary shape and generally parallel to the oxy-fuel flame passage to achieve the same fuel-rich oxy-fuel flame overlying a fuel-lean highly radiative flame.
  • FIG. 1 is a schematic perspective view of an apparatus according to the present invention.
  • FIG. 2 is an enlarged front elevational view of the burner of FIG. 1.
  • FIG. 3 is a schematic view representing a horizontal cross-section through the passages of the precombustor of FIG. 1.
  • FIG. 4 is a vertical cross-section of the passages of the precombustor of FIG. 1.
  • FIG. 5 is a perspective view illustrating the process of the present invention.
  • FIG. 6 is a schematic vertical cross-section of a combustion system according to the present invention.
  • FIG. 7 is a plot of flame velocity against staging for an apparatus according to the present invention.
  • FIG. 8 is plot of flame velocity against staging for an alternate embodiment of the present invention.
  • FIG. 9 is a plot of flame velocity against staging for another embodiment of the present invention.
  • FIG. 10 is a plot of the measured NO emissions against percent oxygen staging for the method and apparatus of the present invention.
  • FIG. 11 is a plot of normalized NO emissions against percent oxygen staging from the data of FIG. 10.
  • FIG. 12 is a plot of normalized NO emissions against percent oxygen staging for a variety of burner operating conditions.
  • FIG. 13 is a schematic top plan view of a glass furnace heated according to the prior art.
  • FIG. 14 is a schematic plan view of a glass melting furnace employing a burner according to the present invention.
  • FIG. 15a is a bar graph depicting relative crown temperatures for conventional oxy-fuel burners and staged combustion according to the present invention.
  • FIG. 15b is a bar graph of relative melt temperatures for conventional oxy-fuel burner and staged oxy-fuel burners according to the present invention.
  • the present invention is directed to a method and apparatus that is an improvement over the method and apparatus shown and described in co-pending U.S. application Ser. No. 08/334,208 filed Nov. 4, 1994, the specification of which is incorporated herein by reference.
  • the present invention is an improvement in the sense that it employs the invention of the copending application in a staged combustion system and process.
  • Oxygen is taken to mean an oxidizer gas with greater than 30% oxygen, preferably 80 to 100% oxygen.
  • Fuel is taken to mean any gaseous hydrocarbon fuel. Natural gas flames are usually not luminous, so the emphasis in the following detailed description is on natural gas as a fuel, however, it is reasonable to expect that the present invention increases flame luminosity of other gaseous fuels.
  • Burner nozzles are taken to mean burner nozzles of various cross-section geometries, where natural gas is introduced through the central nozzle and oxygen around it.
  • Precombustor also sometimes referred to as the burner block, refractory tile, etc.
  • a precombustor is made of a refractory material and its use is to provide a port in a furnace wall for mounting a burner.
  • the internal shape of the precombustor plays a key role in determining flame exit velocity.
  • a precombustor can also protect the burner from corrosive species and high furnace temperatures. The detailed description of the invention addresses the method and the apparatus both with and without a precombustor.
  • the apparatus of the invention shown generally as 10 includes a burner 12 and a precombustor or burner block 14.
  • the burner 12 is a concentric flat flame burner wherein natural gas is conducted down through an inner conduit 16 and oxygen is conducted through the passage defined by inner conduit 16 and outer conduit 18.
  • the fuel e.g. natural gas
  • the apparatus of the present invention includes a staging oxygen passage 22 which is generally elongated in shape, having a shape complementary to the shape of the natural gas passage 16 of burner 12. Staging oxygen is conducted through passage 22 and out through a passage 24 in the burner block 14.
  • the natural gas and the combustion oxygen combine to produce a flame at a discharge end 17 of natural gas passage 16.
  • Staging oxygen exits passage 24 at the same face 21 of burner block 14.
  • the fuel rich oxy-fuel flame combines with the staging oxygen flow after being discharged from discharge end 21 of burner block 14.
  • FIG. 2 shows the discharge nozzle end of the burner 12 wherein the conduit 16 delivers natural gas and the passage between the conduit 16 and the outer conduit 18 is used to deliver oxygen for combustion with the natural gas.
  • FIG. 3 is a top sectional schematic view of the passage for both the flame produced by the burner 12 and the staging oxygen illustrating the angle of divergence for these passages.
  • the angle of divergence is shown as the half angle ( ⁇ /2) being equal to or less than 15%.
  • FIG. 4 is a vertical section through the burner block 14 showing the half angle ( ⁇ /2 being equal to or less than 10°) for the flame and oxygen passages 20, 22 respectively.
  • FIG. 6 shows the invention in schematic form which figure can be used to describe the process of the invention with a burner block.
  • natural gas and combustion oxygen are combined to produce a fuel-rich flame 30.
  • Staging oxygen is introduced beneath the fuel-rich flame to produce a highly radiative fuel-lean flame 32.
  • Circulation patterns are shown by the arrows 31, 33 respectively for the fuel-rich flame and the fuel-lean flame.
  • a highly radiated fuel-lean flame can be produced over a furnace load 34 which can be molten glass as will hereinafter be more fully discussed.
  • staging oxygen is conducted to the apparatus by diverting a portion of the combustion oxygen from the burner used to produce the oxy-fuel fuel-rich flame. The amount of oxygen diversion is referred to as percent staging as will hereinafter be more fully described.
  • a staged combustion method and apparatus produces lower NO X , higher flame luminosity and better flame coverage than is currently available with oxy-fuel burners.
  • the method and apparatus of the present invention can produce flames with more intense radiation directed toward the furnace load, e.g. glass, aluminum, steel, etc, than towards the crown of the furnace. This in turn should improve process efficiency, increase the life of furnace crown refractories, and improve product quality.
  • the natural gas surrounded by oxygen permits the flame to pass through the precombustor without damaging the walls.
  • the reactant nozzle velocities should be kept below 600 ft. per second and should be identical for both natural gas and oxygen to provide optimum results.
  • a discussion of the benefits of oxy-fuel combustion by controlling reactant velocities can be obtained from U.S. Pat. No. 5,199,866; 5,256,058; and 5,346,390 the specifications of which are incorporated herein by reference.
  • Staging oxygen velocity is, in general, lower or similar to the flame velocity to allow formation of a continuous higher-radiation flame zone directed towards the furnace load.
  • the flame having a higher velocity entrains the lower velocity oxygen producing a fuel-lean flame zone as illustrated in FIG. 6.
  • This is in contrast to the widely used high-velocity staging where an oxygen jet creates a localized high-temperature flame zone which usually reduces the overall flame length.
  • the resulting delayed-mixing flame of the present invention having a fuel-rich zone on the top and a fuel-lean zone on the bottom, is much longer, produces lower NO X and radiates more towards the furnace load than a non-staging flame.
  • a range of precombustor diverging angles is used to control the flame.
  • the half angles for the nozzle and the horizontal plane are preferably equal to or less than 15°.
  • the precombustor is used to enable flame acceleration as the volume of reactant, i.e. fuel and oxygen, increases due to temperature increase from combustion. The gases expand and flame velocity reaches maximum for the lowest angle.
  • a divergence half angle of 15° in the combustor compensates for gas expansion and produces minimum acceleration.
  • the preferred flame velocities at the exit end 21 of the burner block 14 are between 30 and 60 ft. per second as the flame exists the precombustor 14. Flame velocities below 30 ft.
  • a straight through or 0° precombustor divergence angle is the best choice for burners firing at low rates, e.g. 1 to 3 Btu/hr.
  • oxygen staging permits control of flame velocity to maintain flame length luminosity and low turbulence or mixing for low NO X operation.
  • a 10° precombustor divergence angle is recommended for higher firing rates up to 6 million Btu/hr.
  • the 10° divergence angle allows for gas expansion and reduces flame acceleration inside the precombustor.
  • FIG. 8 illustrates the preferred operating ranges where the precombustor has a 10° diverging angle. A 15° precombustor diverging angle will produce optimum flame velocity for firing rates up to 12 million Btu/hr.
  • FIGS. 7, 8 and 9 represent performance of preferred embodiments of the present invention.
  • the flame velocities would change if the design parameters are changed such as fuel nozzle width, w/h ratio, and precombustor length.
  • High-temperature tests of the staged-combustion oxygen-natural gas burner produced according to the present invention were conducted in a combustion laboratory furnace. The tests were to determine the effects of oxygen staging on NO X emissions, flame length and luminosity. Temperature of the furnace was maintained at about 2300° F. while measurements were made at different staging levels.
  • the first and last readings were taken under identical conditions to check the reproducibility of the data.
  • An example of a data set is shown in FIGS. 10 and 11 where NO was reduced up to 40% with oxygen staging.
  • the same data set but with normalized NO emissions is shown in FIG. 11.
  • the data normalization should allow comparison of NO emissions at various operating conditions.
  • furnace nitrogen which exact concentration was not measured, needed for NO X formation, came mostly from furnace leaks and, in small quantities, from natural gas. From Table II, it can be seen that the experiments wherein staging was employed, either at 25 or 60% oxygen through the precombustor, had a significant reduction in NO.
  • Table III sets forth the results of a further series of measurements wherein a controlled amount of air, e.g. 5000 scfh at 70° F. was introduced into the furnace.
  • FIG. 12 graphically illustrates the efficiency of lowering NO emissions with staged combustion. As seen from FIG. 12, the NO reduction is about 40% compared to the non-staged operation for any particular set of burner operating parameters with or without additional air.
  • FIG. 13 shows the glass furnace 40 with the conventional burners 42, 44, 46, 48, 50, 52, 56 and 58.
  • burner 42 which utilizes 15% of the fuel utilized in the entire furnace was replaced with a combustion system according to the present invention. Burner 42 is near the pull end 60 of the furnace 40.
  • the objectives of the test were to:
  • the scum blanket is shown as 62 in FIG. 13 and extends almost to the position of the opposed firing burners 42, 58 in the furnace 40.
  • the portion of FIG. 13 indicated as batch indicates the position of batch materials that are unreacted which batch line extends to the position of burner 44.
  • the use of oxy-fuel burners in a glass furnace can cause localized heating immediately under the flames which results in surface reboiling of the glass leading to scum formation.
  • the scum on the glass surface is usually associated with poor overall heat transfer and inefficient melting operations. For some high quality glasses such as television panels and float glass, the glass quality is reduced significantly by the presence of scum on the surface of the melt.
  • a burner system 10 was installed in place of the burner 42 in furnace 40.
  • the average furnace crown temperature was higher when using staged combustion oxy-fuel firing according to the present invention.
  • the average melt bottom temperature was much higher during staged combustion according to the present invention as opposed to conventional oxy-fuel heating of the furnace.
  • the temperature increased significantly when a staged combustion burner was installed. It was also observed that the total furnace fuel consumption, i.e. firing rate trend, was reduced 24 hrs. after the burner according to the present invention was installed. The reasons for fuel flow reduction was the furnace operators concern that the overall furnace temperatures were getting too high.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
US08/523,988 1995-09-05 1995-09-05 Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces Expired - Lifetime US5611682A (en)

Priority Applications (10)

Application Number Priority Date Filing Date Title
US08/523,988 US5611682A (en) 1995-09-05 1995-09-05 Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces
TW085107157A TW316286B (es) 1995-09-05 1996-06-14
KR1019960026682A KR100249051B1 (ko) 1995-09-05 1996-07-02 질소 산화물을 적게 발생시키는 스테이지형 산소 연료 버너, 연소 시스템
CA002184459A CA2184459C (en) 1995-09-05 1996-08-29 Low-nox staged combustion device for controlled radiative heating in high temperature furnaces
BR9603633A BR9603633A (pt) 1995-09-05 1996-09-02 Queimador escalonado de oxi-combustível com baixo nox para aquecimento radioativo controlado em fornos de alta temperatura sistema queimador e processo de produção de chama
ES96114157T ES2186751T3 (es) 1995-09-05 1996-09-04 Quemador de combustion escalonada con baja emision de nox para el cal entamiento controlado por radiacion de los hornos de temperatura elevada.
EP96114157A EP0762050B1 (en) 1995-09-05 1996-09-04 Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces
DE69624762T DE69624762T2 (de) 1995-09-05 1996-09-04 Brenner mit geringer NOx-Emission für stufenweise Verbrennung mit kontrollierter Abgabe von Strahlungswärme in Hochtemperaturöfen
ZA9607469A ZA967469B (en) 1995-09-05 1996-09-04 Low-Nox staged combustion device for controlled radiative heating in high temperature furnaces.
CNB961128143A CN1134610C (zh) 1995-09-05 1996-09-05 用于在高温炉中受控辐射加热的低NOx分级燃烧装置

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Application Number Priority Date Filing Date Title
US08/523,988 US5611682A (en) 1995-09-05 1995-09-05 Low-NOx staged combustion device for controlled radiative heating in high temperature furnaces

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US5611682A true US5611682A (en) 1997-03-18

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US (1) US5611682A (es)
EP (1) EP0762050B1 (es)
KR (1) KR100249051B1 (es)
CN (1) CN1134610C (es)
BR (1) BR9603633A (es)
CA (1) CA2184459C (es)
DE (1) DE69624762T2 (es)
ES (1) ES2186751T3 (es)
TW (1) TW316286B (es)
ZA (1) ZA967469B (es)

Cited By (72)

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US5888265A (en) * 1997-12-22 1999-03-30 Praxair Technology, Inc. Air separation float glass system
US5975886A (en) * 1996-11-25 1999-11-02 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Combustion process and apparatus therefore containing separate injection of fuel and oxidant streams
US5980243A (en) * 1999-03-12 1999-11-09 Zeeco, Inc. Flat flame
EP0969249A2 (en) 1998-06-30 2000-01-05 Praxair Technology, Inc. Wide flame burner
US6196834B1 (en) 1998-11-25 2001-03-06 Aga Gas, Inc. Oxy-fuel ignitor
EP1094273A1 (en) 1999-10-18 2001-04-25 Air Products And Chemicals, Inc. Method and apparatus for backing-up oxy-fuel combustion with air-fuel combustion
US6394792B1 (en) 1999-03-11 2002-05-28 Zeeco, Inc. Low NoX burner apparatus
US6519973B1 (en) * 2000-03-23 2003-02-18 Air Products And Chemicals, Inc. Glass melting process and furnace therefor with oxy-fuel combustion over melting zone and air-fuel combustion over fining zone
US6540508B1 (en) 2000-09-18 2003-04-01 The Boc Group, Inc. Process of installing roof mounted oxygen-fuel burners in a glass melting furnace
US6579085B1 (en) * 2000-05-05 2003-06-17 The Boc Group, Inc. Burner and combustion method for the production of flame jet sheets in industrial furnaces
US6582218B1 (en) 2002-06-11 2003-06-24 Air Products And Chemicals, Inc. Self-cooling oxy-fuel through-port burner for protruding into glass furnace atmosphere
US20030175635A1 (en) * 2002-03-16 2003-09-18 George Stephens Burner employing flue-gas recirculation system with enlarged circulation duct
US20030175646A1 (en) * 2002-03-16 2003-09-18 George Stephens Method for adjusting pre-mix burners to reduce NOx emissions
US20030175634A1 (en) * 2002-03-16 2003-09-18 George Stephens Burner with high flow area tip
US20030175632A1 (en) * 2002-03-16 2003-09-18 George Stephens Removable light-off port plug for use in burners
US20030175637A1 (en) * 2002-03-16 2003-09-18 George Stephens Burner employing cooled flue gas recirculation
US20030175639A1 (en) * 2002-03-16 2003-09-18 Spicer David B. Burner employing flue-gas recirculation system
US6659762B2 (en) * 2001-09-17 2003-12-09 L'air Liquide - Societe Anonyme A' Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Oxygen-fuel burner with adjustable flame characteristics
US20040018461A1 (en) * 2002-03-16 2004-01-29 George Stephens Burner with low NOx emissions
US6699029B2 (en) 2001-01-11 2004-03-02 Praxair Technology, Inc. Oxygen enhanced switching to combustion of lower rank fuels
US6699030B2 (en) 2001-01-11 2004-03-02 Praxair Technology, Inc. Combustion in a multiburner furnace with selective flow of oxygen
US6699031B2 (en) 2001-01-11 2004-03-02 Praxair Technology, Inc. NOx reduction in combustion with concentrated coal streams and oxygen injection
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EP0762050A3 (en) 1998-04-15
ZA967469B (en) 1998-03-04
CN1134610C (zh) 2004-01-14
KR100249051B1 (ko) 2000-04-01
ES2186751T3 (es) 2003-05-16
EP0762050A2 (en) 1997-03-12
EP0762050B1 (en) 2002-11-13
CN1151002A (zh) 1997-06-04
CA2184459A1 (en) 1997-03-06
DE69624762D1 (de) 2002-12-19
KR970016274A (ko) 1997-04-28
BR9603633A (pt) 1998-05-19
DE69624762T2 (de) 2003-07-03
TW316286B (es) 1997-09-21
CA2184459C (en) 2000-02-01

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